Ammoxidation process for making dicyanonaphthalene

ABSTRACT

In the process of making dicyanonaphthalene by reacting a di-lower alkylnaphthalene, ammonia and oxygen under ammoxidation conditions, the improvement which comprises carrying out said ammoxidation in the presence of a supported alkali-metal vanadium bronze catalyst, promoted with iron and with a molar ratio of ammonia to dialkylnaphthalene of from at least about 10:1 to about 30:1. The invention also embodies the iron promoted catalyst.

It is known in the art to effect ammoxidation of aromatic hydrocarbonssuch as alkylated benzenes and naphthalenes with ammonia and oxygen toobtain the corresponding nitriles. Wide reaction conditions and numeroustypes of catalysts have been employed for such reactions includingvanadium oxides either alone or promoted with one or more differentmetals. In British Pat. No. 977,755 it is disclosed that alkylatedcompounds generally, but particularly those of the benzene series (e.g.,toluene, the xylenes, etc.) and alkyl-substituted pyridines may beconverted to the corresponding nitriles by ammoxidation using 3 to 10times the stoichiometric ratio of ammonia to hydrocarbon and employingas catalyst an oxygen containing compound with or without promoters suchas oxides of titanium, iron, vanadium and others.

In British Pat. No. 1,319,287 an ammoxidation process for alkylatedbenzene hydrocarbons is disclosed using as catalyst a mixture ofvanadium oxide and molybdenum oxide and the mole ratio of ammonia tohydrocarbon is given desirably as 4 to 14 with the comment that "littlesense lies in employing more than 12 moles of ammonia per mole ofhydrocarbon, since an increase in yield cannot be obtained thereby."

In U.S. Pat. No. 3,433,823 ammoxidation of methyl aromatic compoundssuch as toluene, xylene, methylnaphthalene, 1,4-dimethylnaphthalene, andthe like is disclosed using as catalyst a mixture of a vanadiumpolyphosphate and an oxide of molybdenum, copper, tungsten, thorium,uranium or zirconium and where the ammonia to hydrocarbon mole ratio isgiven as 0.2 to 20, preferably 1 to 10.

The numerous disclosures in the prior art of ammoxidation such as thosegiven above generally consider the alkylated benzenes and alkylatednaphthalenes to be equivalent in their reaction with ammonia and oxygen.However, experimental work has shown that in the case of2,6-dimethylnaphthalene the reaction parameters of the prior art do notenable ammoxidation to be achieved in a manner suitabl

ally viable process. For example, with prior art conditions, the2,6-dicyanonaphthalene is obtained with rather low selectively whichmakes the process of low commercial merit.

In accord with the process of this invention a di-lower alkyl (e.g., C₁to C₄) naphthalene (such as 2,4- and 2,6-dicyanonaphthalene) is obtainedwith very high selectivity (on the order of about 90% or higher) byreacting the dialkylnaphthalene, ammonia, and oxygen under ammoxidationconditions and in the presence of a supported alkali-metal-vanadiumbronze catalyst promoted with an iron compound and employing a moleratio of ammonia to dialkylnaphthalene of from at least about 10:1 toabout 30:1. The ratio of ammonia to hydrocarbon reactant is preferablyvaried with the pressure at which the reaction will be carried out. Whenatmospheric pressure or a pressure of about 5 to 10 psig. is used, theratio used will preferably be about 15:1. When the reaction pressure is30 to 50 psig., then a ratio of about 25 to 30 will preferably beemployed. By using such ratios the maximum selectivity to nitrileproduct will be achieved.

The process of the invention is carried out in either a fixed orfluidized bed of operation at a temperature between about 375° C. and550° C., preferably from about 400° to about 450° C., at atmosphericpressure, or higher; say up to about 100 psig. although about 75 psig.(about 5 atm) is the preferred upper limit. The source of oxygen ispreferably air, but any oxygen source is suitable. The process enablesrather limited amounts of oxygen to be used and this, in turn, isfavorable in that less burn of hydrocarbon reactant occurs. Thus, themole ratio of oxygen to hydrocarbon in the reactant stream will usuallybe stoichiometric (3:1) or less and it is preferable to use from about2.5:1 to about 3.0:1. The ratio of ammonia to hydrocarbon used in theprocess of the invention is critical for obtaining high nitrileselectivity and will be at least about 10:1 and the upper ratio will beabout 30:1.

It will be understood that the contact time for the reactants over thecatalyst will vary over a wide range, but will usually be from about 0.1to 30 seconds preferably about 1 to 10 seconds. The contact timeactually used will depend upon catalyst loading, catalyst volume,temperature and other parameters, and the skilled art worker will haveno difficulty in selecting an appropriate contact time dependent uponthese reaction parameters.

The reactant feed stream, will, of course, contain other materials, asfor example, the inert ingredients of air, recycled2,6-dimethylnaphthalene, and other products associated with the recyclestream. This use of a recycle stream will make possible a still moreefficient process.

In addition to the above required parameters of the process it isessential that a particular type of catalyst be used. It is known in theart that the addition of an alkali-metal compound to vanadium pentoxidewill, when the mixture is heated yield complex materials with anomalousvalencies known as a vanadium bronzes. Such lithium bronzes arediscussed by Volkov et al, Zh. Neorg. Khim: 17 (6): 1529-1532 (1972).Vanadium bronzes with sodium are described by Pouchard et al., Bull dela Soc. Chimique de France, No. 7, pages 274,245 (1968), and No. 11pages 43434348 (1967). Similarly, potassium containing vanadium bronzesare discussed by Holtzberg et al., J. Am Chem, Soc. Vol. 78, pages1536-40 (1956). Lithium bronzes are described by Hardy et al., Bull dela Soc. Chimique de France, No. 4, 1056-65 (1965) and by Reisman et al.Jour. Physical Chemistry 66 1181-85 (1962). Also of interest is thearticle by P. Hagenmuller entitled "Tungsten Bronzes, ComprehensiveInorganic Chemistry" edited by J. S. Bailar, Jr. et al. and published in1973 by Pergamon Press.

These bronze materials are prepared by mixing an appropriatealkali-metal compound (e.g., carbonate, oxalate, etc.) with vanadiumpentoxide and heating the mixture at an elevated temperature for severalhours. Depending upon the amount of alkali metal ion added certainphases will be established in accordance with the particular phasediagram pertinent to the mixture. Thus, for example, the Holtzberg etal. article referred to above describes the potassium bronze system andthe sodium system is shown in the article by Slobodin et al., J. Appl.Chem., (USSR) Vol. 38, pp 799,803 (April 1965). Of the above alkalimetal vanadium bronzes, all of which may be used in the process of theinvention, the preferred bronzes for use as catalysts are the sodiumbronzes and mixtures of the various species also may be employed.Preferred species include Bronze I (Bz I) which has an atomic ratio ofsodium to vanadium of 0.167, Bronze II (BZ II) where the atomic ratio is0.417, and an alpha prime phase (α-phase) where the atomic ratio is0.50. The terms Bronze I and Bronze II are used herein because thesecompounds correspond to the compounds called "first BRONZE" and "secondBRONZE" by Slobovin and Fotiev, Jour. Applied Chemistry (USSR) 38 Vol. 4pg. 799 April 1965 where the first bronze is characterized by having14.3 mole percent of Na₂ O in its composition (as does BZ I) and thesecond bronze has 29.4 mole percent of Na₂ O (as does BZ II). Thesepreferred Bronze I and α'-phase bronzes may be further characterized bythe generic empirical formula Na_(x) V₂ O₅ where x is greater than zeroand equal to or less than 1. Other bronze systems of the Na_(x) V₂ O₅species are known where x is greater than 1 and these are useful in theprocess, but are somewhat unstable and therefore not preferred. The BZ Ispecies may be considered as Na₂ O.V₂ O₄.5V₂ O₅ or Na₀.33 which is showntogether with related members of the series at pages 573 to 575 of theHagenmuller article as α-Na_(x) V₂ O₅ where x varies from 0.22 to 0.40,the "β" designation indicating the particular crystal phase as structureof the compound. The BZ II species may be considered as 5Na₂ O. V₂O₄.11V₂ O₅ or as Na₁ _(+x) V₃ O₈ (x = 0.25) which is isotypic with Li₁_(+x) V₃ O₈ and is shown at pages 584 of the Hagenmuller articlementioned above. The α'-phase is characterized as Na_(x) V₂ O₅ where x =017 to 1.0 (see page 577 of the Hagenmuller article). Alsocharacteristic of the bronzes are their X-ray diffraction patternswherein the strongest lines are as follows:

BZ I: 9.6, 7.3, 4.75, 3.87, 3.47, 3.38, 3.21, 3.11, 3.08, 2.92, 2.90,2.727, 2.55, 2.45, 2.38, 2.18, 1.97, 1.87, 2.803, 1.74, 1.535, 1.492.

BZ II: 6.9, 7.04, 5.81, 3.87, 3.62, 3.50, 3.45, 3.21, 3.10, 3.67, 2.57,2.43, 2.32, 2.27, 2.02, 1.97, 1.96, 1.81, 1.72, 1.86, 1.504, 1.333,1.39.

α'-phase: 11.3, 5.645, 4.82, 4.436, 3.667, 3.456, 2.967, 2.889, 2.799,2.604, 2.436, 2.412, 2.291, 2.0196, 1.889, 1.803, 1.77, 1.689, 1.635,1.592, 1.479.

The α'-prime phase as with the other bronzes may be obtained by themethods described in the literature and placed on the support for use inthe process, or it may be made in situ. This is readily achieved bytreating the BZ II on the support with a reducing atmosphere (e.g.,ammonia) or a stream similar to the hydrocarbon, ammonia and oxygen;e.g., an oxygen to hydrocarbon mole ratio of less than about 3.0.

As indicated the catalyst bronzes may comprise a mixture of the abovediscussed bronzes and preferred catalysts will comprise a mixturepredominant in either BZ II or the α'-prime phase or both. While BZ Iused above is operable, it is preferred in order to keep the carbonoxides to a minimum to avoid having a predominant amount of BZ I in thecatalyst composition.

In order to obtain the iron promoted catalyst used in the invention, anappropriate iron compound is simply added during the catalystpreparation. Preferably, an iron oxide such as Fe₂ O₃ will be employedas the promoter. In one technique Fe₂ O₃ is added to all of the powderedcatalyst ingredients and physically mixed and the mixture pressed intopellets for use. In another technique, a water soluble iron salt (e.g.,iron oxalate) is added and used with the other catalyst ingredients toimpregnate the support. The amount of iron loading on the total catalystwill be from about 0.5% to about 25 mole percent (as Fe₂ O₃) of thecatalyst expressed as oxides (e.g., V₂ O₅ plus Na₂ O plus Fe₂ O₃), andfrom about 0.5 to about 15% as iron oxide is preferred.

The catalyst support used in the process of the invention will becomprised of α-alumina. α-alumina is well known in art and isexemplified by natural corundum and by the synthetic varieties which arecommercially available. These materials have a high density (on theorder of about 0.75 to 1.0 gm/cc.) and very low surface area (on theorder of 6m² /gm or less). Generally the α-alumina will contain enoughsodium ions so that the sodium bronzes may be made without any additionof sodium or other alkali metal compounds. But if insufficient sodium ispresent, enough may be added to give the desired bronze. In making thesupported catalyst all that is required is to make an aqueous slurry ofpowdered (170 mesh or finer) α-alumina, alkali metal salt (preferablycarbonate) and V₂ O₅, evaporate off the water, pelletize and calcine thepellets at about 500°-600° C. for several hours, while passing a slowflow of air through the furnace. Alternatively, and preferably, thecatalyst may be placed on the support by an impregnation technique wherean aqueous vanadium oxalate solution containing the appropriate amountof alkali metal is deposited onto the α-alumina support, which method iswell known in the art.

As pointed out above, in making the catalyst, alkali metal ions (usuallyin the form of the carbonate) are added to ensure that a bronze isformed. In a particularly preferred catalyst system where asodium-vanadium bronze is desired, the amount of sodium ion employed tomake the catalsyt will be at a ratio of sodium to vanadium of 0.30 andsuch catalyst appears to be of high bronze purity devoid of extraneousmaterials which might degrade catalyst performance.

As indicated, the catalyst support will be comprised of α-alumina butmay contain other components such as silica and other metal oxides aswell as the normal contaminants found in α-alumina. However, at leastabout 75% by weight of the support will be α-alumina.

The amount of catalyst on the support (e.g., catalyst loading) will befrom about 0.5 to about 20% by weight, preferably about 3 to about 8%.The surface area of the catalysts used in the process is generally quitelow being less than 10m² /gm and usually 1 to 5m² /gm. Pore volume ofthe catalyst is such that the major proportion of the pores havediameters less than about 1 micron, being on the order of about 0.2 to1.0 micron.

After the iron promoted BZ I or a promoted mixed BZ I and BZ II catalystis prepared, but before its use, it is preferred to age the catalyst bya heat treatment at about 500° to about 750° C. for 3 to 4 hours inorder to convert most, if not all of the BZ I to the preferred BZ II.

The catalyst composition of the invention is thus an alkali metalvanadium bronze promoted with iron and is preferably a promoted BronzeII or α-prime phase. The catalysts are preferably pelletized for use,but may also be employed in powder form.

The ammoxidation is carried out preferably in conventional apparatus,the reaction gases passing over the catalyst at reaction temperature andthe effluent gases separated into the appropriate product and by-productstreams. Particular advantages of the process of the invention reside in(a) low formation of carbon oxides, (b) very high selectivity forformation of dinitriles, (c) low oxygen to hydrocarbon ratios, (d)dealkylation is minimized and (e) a relatively low ammonia tohydrocarbon ratio may be used. In order to further describe andillustrate the invention the following examples employing2,6-dimethylnaphthalene as the hydrocarbon are given:

PREPARATION OF CATALYSTS Method A

The α-alumina support is ground into a fine powder having a particlesize of about 170 mesh or less and the appropriate amount of Fe₂ O₃ andV₂ O₅ added to it. If analysis shows that the amount of alkali metal inthe α-alumina is insufficient the desired amount sodium carbonate orother alkali metal salt is added. The mixture is then ground dry andthen water is added and the mixture further agitated to make a slurry;the slurry is poured into a evaporating dish and evaporated to dryness.The dry residue is mixed further to break up agglomerates and wateradded to make a paste which is formed into pellets are then calcined at540° C. for about 4 hours while air at the rate of 2.5 l/min is passedthrough the furnace. After cooling the catalyst pellets are ready foruse.

Method B

Granulated alumina (8 - 16 mesh) is heated at 1300° C. for 4 hours.Ferric oxalate and vanadium pentoxide are suspended in 5 parts of water,heated to 80° C., and oxalic acid is added slowly to obtain ablue-colored vanadium oxalate solution. Sodium carbonate is added andthe alumina is also placed in the solution. The mixture is dried over awater bath with agitation. While air is pumped in, it is indurated in afurnace at 400° C. for 16 hours to obtain the catalyst ready for useafter cooling.

EXPERIMENTAL PROCEDURES

An appropriate quantity of catalyst (with or without inert diluent,e.g., quartz) is placed in a fixed bed quartz reactor (1 1/4 inches indiameter and 24 inches long). Inert packing above the catalyst serves asa preheater section and a small amount (about 1-2 inches) of similarinert packing is placed in the bottom of the reactor to support thecatalyst in the reaction zone. The upper end of the reactor is equippedwith an assembly having multiple openings through which the hydrocarbon,ammonia, and air (or oxygen-helium or oxygen-nitrogen mixtures) can bemetered. The reactants can be mixed in this "mixing chamber" or premixedand then fed into the reactor which is operated at essentiallyatmospheric pressure. The rate of gas flow is adjusted so as to producethe desired contact time at a given reaction temperature over a givenvolume of catalyst.

The effluent gases are passed from the reactor into a chilled flaskwhere the products were collected along with ammonium carbonate andwater. The remaining escaping gas is passed through a cold water cooledcondenser, a drying tube, an ascarite tube, and finally captured in alarge polyvinylchloride bag.

The analysis of the organic layer, water layer, gas sample from the bag,and the weight increase of the ascarite tube (due to CO₂ not bound up asammonium carbonate) enables calculation of the results (i.e.,conversion, carbon balance, yield, etc.).

EXAMPLES 1-7

Using the above described procedure a catalyst of a sodium-vanadiumbronze (BZ II) on α-alumina containing Fe₂ O₃ is prepared. The datashown in Table I indicates the parameters of the process and the datawhich is obtained.

                                      TABLE I                                     __________________________________________________________________________    AMMOXIDATION OF 2,6-DIMETHYLNAPHTHALENE (DMN) WITH A                          BRONZE II CATALYST PROMOTED WITH IRON*                                                           Catalyst                                                                              Contact                                                                            Mole Mole       Combined                            Temp.       Time on Stream                                                                         Time Ratio                                                                              Ratio      Nitrile                       Ex. No.                                                                             (C °)                                                                       Pressure                                                                             w/o Regeneration                                                                       (Sec.)                                                                             O.sub.2 /DMN                                                                       NH.sub.3 /DMN                                                                       % Conv.                                                                            Selectivity                   __________________________________________________________________________    1     400  1 Atm. 1.0      2.0  2.4  20.0  45   98.5                          2     400  1 Atm. 3.0      2.0  2.9  18.3  29   95.8                          3     400  1 Atm. 6.2      2.0  2.9  18.2  25   97.2                          4     431  1 Atm. 7.2      1.9  2.8  19.9  35   95.1                          5     431  1 Atm. 12.1     1.9  2.7  20.1  36   93.8                          6     451  30 psig.= /                                                                          1.0      1.8  3.0  29    29   90.8                          7     451  30 psig.= /                                                                          7.0      1.9  2.9  29    37   94.1                          __________________________________________________________________________     *Catalyst: V.sub.2 O.sub.5 :Na.sub.2 O:Fe.sub.2 O.sub.3 (ca. 4:2:1); ca       15% Fe.sub.2 O.sub.3 ; supported on α-Al.sub.2 O.sub.3                  =/Run in fixed bed Stainless Steel reactor                               

EXAMPLES 8-12

In a series of experiments similar to the above carried out at 6 psig.the results obtained under the reaction conditions are shown in TableII.

                                      TABLE II                                    __________________________________________________________________________    AMMOXIDATION OF 2,6-DMN                                                       CATALYST:                                                                              5 Wt. % Sodium Vanadium Bronze containing 25 Mole %                               Fe.sub.2 O.sub.3                                                 CONTACT TIME:                                                                          2.3 to 2.5 Seconds                                                   PRESSURE:                                                                              6 PSIG.                                                                           Catalyst on Mole Mole                                                         Stream Time w/o                                                                           Ratio                                                                              Ratio %                                         Ex. No.                                                                             Temp (° C)                                                                    Regeneration (Hrs).                                                                       O.sub.2 /DMN                                                                       NH.sub.3 /DMN                                                                       Selectivity                               __________________________________________________________________________    8     403    28.7        2.4  9.7   92.8                                      9     403    27.8        3.0  14.6  95.2                                      10    403    15.4        2.6  18.9  97.4                                      11    402    10.6        2.6  26.2  97.5                                      12    448    36.3        2.3  21.2  97.6                                      __________________________________________________________________________

The data shown in Table III represents the average selectivity,conversion and plant yield of a series of runs made with and without theiron promoter. As can be seen from the results shown in the table, theiron does give an improvement which in plant operations would be ofsignificant value.

                                      TABLE III                                   __________________________________________________________________________    2,6-DMN AMMOXIDATION WITH Fe.sub.2 O.sub.3                                    MODIFIED SODIUM VANADIUM BRONZE CATALYST                                      VERSUS UNMODIFIED BRONZES                                                     Temperature: 450°C.                                                                      Pressure: 30 Psig. (Stainless                                                 Steel Reactor)                                              Mole Ratio NH.sub.3 :DMN: 29:1                                                                  Mole Ratio O.sub.2 :DMN = 3:1                                         (Average)                                                                             (Average)                                                                             (Average)                                           Catalyst  Selectivity (%)                                                                       Conversion (%)                                                                        Plant Yield (*%)                                    __________________________________________________________________________    Sodium-vanadium                                                               8 Wt. % Bronze                                                                          92.3    33.5    87.5                                                + 15 mole % Fe.sub.2 O.sub.3                                                  Sodium-vanadium                                                               8% (wt.) Bronze                                                                         91      36      85                                                  + 5 mole % Fe.sub.2 O.sub.3                                                   Sodium-vanadium                                                               8 Wt. % Bronze                                                                          89.5    30      83.4                                                (No added Fe.sub.2 O.sub.3)                                                   __________________________________________________________________________

The invention claimed is:
 1. An ammoxidation process for preparing2,6-dicyanonaphthalene from 2,6-dimethylnaphthalene which comprisesreacting said dimethylnaphthalene and ammonia at a temperature of fromabout 375° to about 550° C. in the presence of added oxygen, the molarratio of ammonia to dimethylnaphthalene being from at least about 10:1to about 30:1 and the catalyst for said reaction comprising at leastabout 0.5 to 20% by weight of an alkali metal vanadium bronze supportedon α-alumina and promoted with an iron compound in an amount from about0.5 mole percent to about 25 mole percent of the catalyst expressed asoxides.
 2. An ammoxidation process for preparing 2,6-dicyanonaphthalenefrom 2,6-dimethylnaphthalene which comprises reacting saiddimethylnaphthalene and ammonia at a temperature of from about 400° toabout 450° C. in the presence of added oxygen, the molar ratio of oxygento dimethylnaphthalene being from about 2:1 to about 3:1, the molarratio of ammonia to dimethylnaphthalene being from about 15:1 to about30:1, and the catalyst for said reaction comprising at least about 0.5to 10% by weight of an alkali metal vanadium bronze supported onα-alumina and promoted with Fe₂ O₃ in an amount of from about 0.5 toabout 15 mole percent of the catalyst expressed as oxides.
 3. Theprocess of claim 2 where the catalyst is a sodium vanadium bronze. 4.The process of claim 3 where the catalyst is predominantly BZ II or theα-prime phase.
 5. The process of claim 3 operated in a fixed bed mode ata pressure of from about 15 to about 50 psig.
 6. The process of claim 5where the catalyst is predominantly BZ II.
 7. The process of claim 5where the catalyst is predominantly the α-prime phase.
 8. The process ofclaim 5 where the catalyst is a mixture of BZ II and the α-prime phase.9. The process of claim 2 operated in a fluidized bed mode at 1 to about5 atmospheres and the catalyst is a sodium vanadium bronze.
 10. Theprocess of claim 9 where the catalyst is predominantly BZ II.
 11. Theprocess of claim 10 where the catalyst is predominantly the α-primephase.
 12. The process of claim 10 where the catalyst is a mixture of BZII and the α-prime phase.